Continuous steel production and apparatus

ABSTRACT

A process for continuous refining of steel via multiple distinct reaction vessels for melting, oxidation, reduction, and refining for delivery of steel continuously to, for example, a tundish of a continuous caster system, and associated apparatus.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims the benefit of U.S. Provisional Application Ser.No. 60/678,833, filed May 6, 2005, the entire content of which is herebyincorporated herein by reference.

STATEMENT OF GOVERNMENT INTEREST

This invention was made with government support by the Department ofEnergy under cooperative agreement number DE FC36-03ID14279. Thegovernment has certain rights in the invention.

FIELD OF THE INVENTION

This invention relates to a method for continuously producing steel byintegrated and continuous melting, refining, and delivering steel to,for example, a tundish of a continuous caster.

BACKGROUND OF THE INVENTION

A number of processes have been proposed for continuous production ofsteel dating back to the 1860s. “Continuous” in this context has beenused to describe processes which semi-continuously charge hot metal orscrap and deslag while periodically tapping steel into ladles. It hasbeen used to describe processes which continuously utilize variousvessels while continuously tapping steel into ladles, though in certainaspects there are interruptions somewhere in the melting, refining, ortransporting operations. And it has been used to describe fullycontinuous processes which continuously transport steel from melting,through refining, to molding in a continuous caster without interruptionin the flow of steel.

Continuous steelmaking processes have not received general acceptance inthe industry because they could not compete with conventionalsteelmaking technology. Frequent improvements in basic oxygen furnaces(BOFs), electric arc furnaces (EAFs), ladle metallurgy furnaces (LMFs),and other secondary treatment facilities have provided production andquality flexibility perceived as more profitable than commercializationof new and risky continuous steelmaking processes which have beenproposed, although some processes have been extensively tested.

Processes that resemble non-equilibrium CSTRs or PFRs in certainrespects have suffered from lack of control and failure to promisesubstantially lower meltshop costs than conventional batch operations.Most of these processes have been designed to continuously utilize theequipment and to perform one major refining step (e.g., desulfurization)while tapping steel into a ladle as practiced in batch operations. Theutilization of most batch reactors is close to one hundred percent,eliminating substantially any advantage of processes that are not fullycontinuous and do not completely prepare the steel for introduction tocontinuous casters.

A large number of continuous steelmaking processes were introduced inthe 1960s just after the peak of the open hearth furnace (OHF) processand during the time of rapid BOF development and growth. The number ofnew continuous steelmaking processes declined after the 1960s as BOF andEAF steelmaking processes were optimized and improved through theintroduction of LMFs. Today, BOF, EAF, and LMF are mature technologiesoperating close to optimum, allowing for only marginal futureimprovements in these processes. A major decrease in meltshop costs istherefore only possible with new, revolutionary processing.

U.S. Pat. No. 6,155,333 describes a scrap-based process whichcontinuously charges scrap and continuously operates at near-equilibriumsteady state conditions during melting, decarburization, anddephosphorization. However, the overall process is only semi-continuousbecause periodic tapping of the furnace interrupts the overall steadystate operation.

In order to offset risks of investing in new technology, a newsteelmaking process needs to have a potential to significantly reducemeltshop costs, and be reliable. There is a need, therefore, for a fullycontinuous process which can produce high quality steel at significantlylower cost with sufficient reliability and benefits to justifycommercialization.

SUMMARY OF THE INVENTION

Briefly, therefore, the invention is directed to an apparatus forcontinuous refining of steel comprising a melting furnace, for meltingiron-bearing material into molten metal, the furnace comprising a heatsource, a melting furnace inlet for continuously receiving theiron-bearing material, a melting vessel in communication with said inletfor melting the iron-bearing material into molten metal and holding themolten metal, and a melting furnace outlet for discharging the moltenmetal continuously from the melting vessel simultaneously with themelting furnace inlet's continuously receiving the iron-bearingmaterial; an oxidizer for oxidizing oxidizable elements in the moltenmetal, the oxidizer having a chemically oxidizing environment andcomprising an oxidizer inlet for continuously receiving molten metaldischarged from the melting furnace outlet, an oxidizing vessel incommunication with the oxidizer inlet for holding molten metal, and anoxidizer outlet for continuously discharging the molten metal from theoxidizer simultaneously with the oxidizer inlet's continuously receivingthe molten metal discharged from the melting furnace outlet; and areducer for deoxidizing and desulfurizing the molten metal, the reducerhaving a chemically reducing environment and comprising a reducer inletfor continuously receiving the molten metal discharged from the oxidizeroutlet, a reducer vessel in communication with the reducer inlet forholding molten metal, and a reducer outlet for continuously dischargingthe molten metal from the reducer simultaneously with the reducerinlet's continuously receiving the molten metal discharged from theoxidizer outlet.

In another aspect, the invention is directed to a process for continuousrefining of steel comprising continuously feeding iron-bearing materialinto a melting furnace and melting the iron-bearing material into moltenmetal therein, wherein the melting furnace comprises a heat source, amelting furnace inlet for continuously receiving the iron-bearingmaterial, a melting vessel in communication with said inlet for meltingthe iron-bearing material into the molten metal and holding the moltenmetal, and a melting furnace outlet; discharging the molten metalcontinuously through the melting vessel outlet simultaneously with themelting furnace inlet's continuously receiving the iron-bearingmaterial; continuously receiving the molten metal discharged through themelting vessel outlet into an oxidizer for oxidizing oxidizable elementsin the molten metal, the oxidizer having a chemically oxidizingenvironment and comprising an oxidizer inlet for the continuouslyreceiving molten metal discharged through the melting furnace outlet, anoxidizing vessel in communication with the oxidizer inlet for holdingmolten metal, and an oxidizer outlet; oxidizing oxidizable elements inthe molten metal in the oxidizer vessel; discharging the molten metalcontinuously through the oxidizer vessel outlet simultaneously with theoxidizer inlet's continuously receiving the molten metal dischargedthrough the melting furnace outlet; continuously receiving the moltenmetal discharged from the oxidizer vessel outlet into a reducer fordeoxidizing and desulfurizing the molten metal, the reducer having achemically reducing environment and comprising a reducer inlet forcontinuously receiving the molten metal discharged through the oxidizeroutlet, a reducing vessel in communication with the reducer inlet forholding molten metal, and a reducer outlet; and discharging the moltenmetal continuously through the reducer vessel outlet simultaneously withthe reducer inlet's continuously receiving the molten metal dischargedthrough the oxidizer outlet.

Other objects and features of the invention will be in part apparent andin part pointed out hereinafter.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a perspective view of the steelmaking apparatus of theinvention;

FIG. 2 is a perspective view of a melting furnace component of theapparatus;

FIG. 2A is a section view taken along line 2A-2A;

FIG. 3 is a perspective view of an oxidizer component of the apparatus;

FIG. 3A is a section view taken along line 3A-3A;

FIG. 4 is a perspective view of a reducer component of the apparatus;

FIG. 4A is a section view taken along line 4A-4A;

FIG. 5 is a perspective view of a finisher component of the apparatus;

FIG. 5A is a section view taken along line 5A-5A; and

FIG. 6 is a perspective view of a tundish component of the apparatus.

DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS

The present invention is based on the incorporation into steelmaking ofnear-equilibrium CSTRs. The reduction of the necessary chemicalconversion by using scrap or other low-impurity, iron-based material,coupled with the improvements in the chemical conversion possible byusing a series of near-equilibrium CSTRs, improve the possibility ofeconomic continuous operation. Tundish operations which feed thecontinuous caster are improved with a continuous, steady, and reliablyconsistent supply of steel from the three vessels that resemblenear-equilibrium CSTRs.

The apparatus and process of the present invention are designed toreplace steelmaking operations which employ an EAF, LMF, and continuouscaster. The process allows for substantial variation in production ratesuch as between about 30 t/hr and about 220 t/hr. The process canoperate for one week or longer without interruption of steel productionand with an expected weekly maintenance downtime on the order of 8 to 12hours.

Turning to FIG. 1, the apparatus comprises five interconnected vesselsincluding in sequence a melting furnace 20, an oxidizer 30, a reducer50, a finisher 70, and a tundish 90. Scrap is continuously charged toand melted in the melting furnace, which is a modified Consteel® AC EAF.The scrap is preheated in the Consteel® conveyor. In one embodiment thefurnace charge is delivered to the furnace as described in U.S. Pat. No.6,450,804, the entire disclosure of which is expressly incorporatedherein by reference. In the melting furnace melting is achieved withelectrical energy and chemical energy from exothermic reactions such asthe combination of C and O to form CO, the oxidation of Al to alumina,and other oxidation reactions. Preliminary decarburization anddephosphorization are performed in the melting furnace 20 while a foamyslag is maintained. Further decarburization and dephosphorization areperformed in the oxidizer 30. Near-equilibrium conditions allow for justpartial deoxidation in the oxidizer, if desired, depending on the targetcarbon concentration. In the reducer 50 the molten metal is continuouslydeoxidized, desulfurized, and optionally alloyed. In the finisher 70 themolten metal is subject to final trimming, additional desulfurization,inclusion flotation, and homogenization. From the finisher 70 the moltenmetal flows continuously into the tundish 90, which continuously feedsthe continuous caster. The discharge from the finisher is optionallysuitable for steel casting operations which do not involve a tundish andcontinuous caster. Oxidizing conditions are maintained in the meltingfurnace and oxidizer; and reducing conditions are maintained in thereducer and finisher.

The series of oxidizer 30 and reducer 50 reactors with similarnear-equilibrium conditions allows for optimum refining and forminimization of variations in fluid flow (residence time distributions)and composition (chemistry, inclusion concentration). This contributesto the reliability and flexibility of the process. The sequentialrefining and near-equilibrium, steady-state operation of the processallows for increased refining. It also allows for reduced alloyconsumption and flux consumption in comparison to EAF-LMF processes. Forinstance, it is predicted that no oxidizing slag would carry over invessels with reducing slag, as it is currently experienced during thetapping of furnaces.

With respect to the melting furnace, in a preferred embodiment it is amodified version of the EAF depicted in FIGS. 10 and 11 of U.S. Pat. No.6,155,333, the entire disclosure of which is expressly incorporatedherein by reference. As shown in FIGS. 2 and 2A, the melting furnace 20is equipped with an eccentric bottom tapping (EBT) bottom tap unit 29including melting furnace outlet 25 positioned so that it is level withthe lowest point 28 of the furnace vessel, as indicated. There is aconstant material fill height between about two and about four feet,though all units are shown empty here. These features eliminate orsubstantially eliminate carry-over slag during steady-state operation,and allow for complete draining of the melting furnace into the oxidizerwithout tilting the furnace vessel. Flow of molten material out of themelting furnace is through a melting furnace outlet 25, here shownhaving a shroud and a side port. Flow is regulated, preferably by aslide gate 24 having hydraulic piston 23. There are also electrodes 27and EBT maintenance door 26. The inner diameter of the melting furnacevessel is between about 10 and about 15 feet. In one preferredembodiment the melting furnace vessel has a constant material fillheight of about 2.3 feet and an inner diameter of about 13.8 feet.

Scrap and flux are charged continuously into the EAF through meltingfurnace inlet 22, which communicates with a conveyor system (not shown).Direct reduced iron (DRI) or other scrap substitutes may also be used inaddition to or instead of scrap, or a partial charge of hot metal as itis practiced with some EAF furnaces. The charge to the melting furnacein some applications, but not all applications, has a carbon content ofless than 0.5%, preferably less than about 0.3%. The scrap and flux arepreferably preheated to reduce the required size of the vessel byminimizing electrical energy requirements. Molten metal is continuouslytapped from the bottom via outlet 25. By charging and tappingcontinuously, the furnace is operable in 100% power-on condition with aconstant full furnace. For example, in one preferred embodiment there isa constant 55-ton liquid heel. The power supply is preferably AC toavoid the need for a bottom electrode.

The oxidizer 30 shown in FIGS. 3 and 3A performs additionaldecarburization and dephosphorization. It has an inside diameter ofbetween about 4 and about 6 feet; 4.9 feet in the preferred embodiment,with a 27-ton capacity. Steel enters through an oxidizer inlet 32 andassociated inlet chute 31, which in the preferred embodiment is 1.3 ftwide by 4 feet long. Entrance 45 in communication with chute 31 islocated off-center to the oxidizer vessel, to produce a swirl in thesteel bath and minimize risk of short-circuiting, i.e., of materialpassing directly from the oxidizer inlet system to the oxidizer outlet36 without sufficient residence time in the vessel to be refined andhomogenized with the vessel contents. The depth of the bath is betweenabout 4 and about 7 feet; about 5.4 feet in the preferred embodiment.There is between about 3 and about 5 feet of free space above the bath;3.7 feet in the preferred embodiment. The bath is stirred by injectingargon through plugs 44 (only one of three shown here) on the bottom ofthe vessel. The preferred embodiment employs three plugs to ensureconstant and homogenous stirring even if one plug fails. The plugs areporous and produce small bubbles, promoting degassing reactions and theflotation of inclusions as well as increasing the gas/steel interface.

The oxidizer 30 has an oxidizer outlet 36 associated with an outletchute (not shown) which in the preferred embodiment is 1.3 feet wide and5.5 feet long. There are accompanying slide gate 42 and hydraulic piston43. Outlet 36 is located so as to remove steel from the oxidizer vesselnear the bottom to reduce risks of short circuiting and slag carryover.Less height is required than if the oxidizer outlet 36 were on thebottom of the vessel. For emptying the vessel for maintenance, if needbe, there is an emergency slide gate 40. Or the steel can be pouredthrough the oxidizer inlet chute 31 by removing and tilting the vesselwith a crane. Hooks 41 and trunnions 35 and similar features of this andother vessels are used for this purpose. The oxidizer is supported bylegs 42.

The inward stream of steel within the oxidizer inlet chute 31 creates anoutward flow of slag on the upper surface. Spent slag is continuouslyremoved at the oxidizer inlet, for example, via the oxidizer inlet chute31 by this outward flow, and is optionally mechanically assisted, suchas by a rake or auger mechanism (not shown). Thus slag is continuouslytransported to an overflow and into a slag pot below the oxidizer inletchute 31. It is directed there by the apron shown associated with inlet31, similar to the apron 37 associated with the oxidizer outlet.Off-gases are evacuated through a duct 33 in a removable roof that restson the main vessel. Duct 33 is in communication with rim 34 whichencloses the upper lip of the oxidizer to minimize intake of atmosphericair during off-gassing. There is a door 38 in the roof that providesaccess for observation and maintenance. If desired, alloying elementsand fluxes are delivered through the alloy chute 39 that is locatedabove the center of the top surface.

The steel is then deoxidized, desulfurized, and alloyed in the reducer50 illustrated in FIGS. 4 and 4A. Steel enters the reducer vessel via areducer inlet 51 which, similar to the oxidizer inlet, has an associatedinlet chute 52 which is off-center to impart swirling and enhancehomogenization. Slag exits at the reducer inlet, for example, via thereducer inlet chute 52. The reducer vessel 55 has a conical shape withan upper inner diameter between about 5 and about 8 feet, a lower innerdiameter between about 0.5 and about 3 feet, and an operating depth ofabout 5 to about 9 feet of steel, with about 3 to about 5 feet of freespace above the steel level. In a preferred embodiment, the upper innerdiameter is about 6.6 feet, the lower inner diameter is about 1.3 feet,the operating depth is about 7.2 feet, the free space is about 3.7 feet,and the top surface area of the steel bath about 34 ft², which is almosttwice the top surface area in the oxidizer. The steel is stirred viaargon through a porous plug 67 in the bottom of the vessel. The conicalshape increases the fraction of the steel that is highly stirred, andincreases the proportion of the steel in the vessel which is at theslag/metal interface in comparison to ladle vessels. This configurationmaximizes the energy input into the steel, reaction rates, sulfurremoval, temperature homogenization, chemistry homogenization, andproduction rates. The reducer outlet 54 has a shroud with a side port asshown, and is at the bottom of the reducer vessel 55. Access forinspection and maintenance is available through doors 57 and 57′. Thereis a slide gate 64 and hydraulic piston 63 for operation thereof. Thereducer is supported by legs 66. There is continuous de-slagging throughthe reducer inlet chute 52 and associated apron 53 as with the oxidizer.There is a chute 59 for introduction of alloying elements and flux, anda door 58 for maintenance and observation. There is off-gas system 61which preferably completely encloses the vessel roof joint around thesides via rim 62 to minimize pulling in of air from the surroundingatmosphere during release of off gas.

The oxidizer 30, reducer 50, and finisher 70 each has a vessel wallwhich is 16 inches thick in the preferred embodiment, allowing forplacement of a 9-inch thick refractory lining, such as a resin-boundedmagnesia refractory lining, a 2.5-inch back-up lining, and 2.5-inchthick insulating bricks, in addition to the structural support of asteel shell. The rest of the vessel is lined with a resin-boundedmagnesia. The oxidizer vessel and reducer vessel each has a slag linelined with a magnesia-graphite refractory at the level of the slag inthe vessel. These are low porosity materials to resist penetration.Refractory losses associated with thermal cycling, erosion, andcorrosion are reduced as compared to ladle processes because consistenttemperature and chemical conditions exist in each vessel. Theelimination of frequent forceful tapping streams and cleaning of ladleswith oxygen also reduces erosion and corrosion.

Final alloying/trimming is accomplished in the finisher 70 shown inFIGS. 5 and 5A, as is some additional desulfurization. The finisher 70is similar to the oxidizer 30. The finisher has finisher inlet 71 withassociated inlet chute 72, and finisher outlet 73 with slide gate 74 andassociated hydraulic piston 75. Slag exits at the finisher inlet, forexample, via the finisher inlet chute 72. Entrance 86 in communicationwith chute 72 is off-center as with the oxidizer and reducer vessels.There is off-gas system 79 on the finisher vessel 76 similar to theoff-gas system with the reducer, which preferably completely enclosesthe vessel roof joint around the sides via rim 80 so that introductionof air from the surrounding atmosphere is minimized during release ofoff gas. Steel is tapped through a bottom tap hole into the outlet 73,which allows for complete emptying of the finisher during grade changes.Trunnions 81 are available for transportation. Door 77 permitsobservation and maintenance access. Chute 78 is for alloy and fluxadditions. Porous plug 85 (one of, for example, three plugs) permitsintroduction of argon for stirring.

During normal operation, the steel bath level in the finisher remainsconstant, with continuous argon bubbling at a low flow rate, such as 7scfm. This maximizes cleanliness, and chemistry and temperaturehomogeneity. Auxiliary heating of the steel during refining is notrequired during normal operation of the continuous steelmaking processbecause of the shorter residence time in comparison to other systems.For example, the average residence time for a segment of material in theentire system (entry furnace to exit tundish) is approximately one hourduring a production (flow) rate of 150 t/hr. A non-contact twin plasmatorch or the like can be used with access through the roof door if thereare unexpected delays requiring heating.

There are slag pots and working platforms 96 (FIG. 1) associated witheach of the three vessels. Each slag pot collects slag from one inletchute and from the outlet chute of the previous vessel.

The operation of the melting furnace involves continuous loading ofscrap onto the conveyor, continuous injection of carbon and oxygen, andcontinuous introduction of flux, to maintain a constant foamy slag withdeslagging out the door. There is continuous tapping of steel into theoxidizer. After steel leaves the melting furnace 20 it cascades throughthe three refining components 30, 50, and 70 before entering the tundish90, shown here as a delta tundish. Tundish 90 comprises inlet 91,tundish vessel 92, and molds 93, from which exit semi-finished steelbillets 94. The treatment of the steel in each refining vessel includesperiodic addition of fluxes to all vessels, and periodic addition ofalloying elements at least to the finisher, and optionally to thereducer and oxidizer. The additions are, for example, every two to threeminutes. There is continuous removal of slag into the slag pots. In thepreferred embodiment, the slag pots hold approximately six tons of slag,such that they are replaced roughly every eight hours.

With respect to the tundish 90, it continually receives steel from thefinisher, so there are no ladle changes. Advantageously, therefore,there are no ladle changes, no significant temperature fluctuations, andno significant molten metal level fluctuations. This decreasesturbulence and reoxidation, and improves the cleanliness of the caststeel. Periodic or continuous temperature and chemistry measurements aretaken, thus allowing sufficient time for corrective action.

Each of the five vessels works as a thermodynamic buffer due tonear-equilibrium reactions, and the series of reactors provides anopportunity to offset variations through differentiated refining andalloying in each vessel.

During start-up, the oxidizer, reducer, finisher, and tundish arepreheated, for example with natural gas burners. A bucket of scrap ischarged directly to the melting furnace to have a liquid heel in placebefore scrap is transported by conveyor into the melting furnace. Whenthe liquid level in the melting furnace reaches its operating height,the scrap supply is temporarily stopped to superheat the steel so thesubsequent vessels can be filled without solidification of the steeltherein. The melting furnace outlet slide gate is opened after the steelin the melting furnace is superheated, and steel flows into theoxidizer. After the oxidizer is filled, steel flow is stopped, ifnecessary, until the desired steel and slag chemistries are achieved inthe oxidizer. The oxidizer outlet is then opened to fill the reducer andbegin operation in a continuous mode. Once the reducer is filled, steelflow is halted again, if necessary, until the desired slag and steelchemistries are achieved in the reducer. The reducer outlet is thenopened to fill the finisher. Once the finisher is filled, steel flow isagain halted, if necessary, until the desired slag and steel chemistriesare achieved in the finisher. The finisher exit is then opened and theexit to the tundish is opened to begin continuous operation of theentire system. Temperature can be adjusted as necessary in the reducer,finisher, and/or tundish during the start-up procedure, such as with atwin plasma torch.

During normal operation after start up, with reference to FIGS. 1-5,iron-bearing material is continuously fed into the melting furnace 20and is melted into molten metal therein. The melting furnace inlet 22continuously receives the iron-bearing material. Molten metal iscontinuously discharged through the melting vessel outlet 25simultaneously with the melting furnace inlet's continuously receivingthe iron-bearing material. Molten metal is discharged through themelting vessel outlet 25 into the oxidizer 30 for further refinement ofthe molten metal. The oxidizer has a chemically oxidizing environmentand has the oxidizer inlet 32 for continuously receiving molten metaldischarged through the melting furnace outlet 25. Molten metal isdischarged continuously through the oxidizer outlet 36 simultaneouslywith the oxidizer inlet's continuously receiving the molten metaldischarged through the melting furnace outlet 25. Molten metal isdischarged from the oxidizer vessel outlet into the reducer 50, whichhas a chemically reducing environment. The reducer inlet 51 continuouslyreceives the molten metal discharged through the oxidizer outlet 36.Molten metal is continuously discharged through the reducer outlet 54simultaneously with the reducer inlet's continuously receiving themolten metal discharged through the oxidizer outlet 36. Molten metal isdischarged through the reducer outlet 54 into the finisher 70 via thefinisher inlet 71. Molten metal is continuously discharged through thefinisher outlet 73 simultaneously with the finisher inlet's continuouslyreceiving the molten metal discharged through the reducer outlet 54.

Shut-down of the system begins with halting of the scrap conveyor. Thesteel level in the melting furnace decreases while steel continues toflow to the subsequent vessels. After the melting furnace is completelydrained, the steel level in the oxidizer decreases until its exitchannel is emptied. The oxidizer is then lifted, rotated, and tilted byan overhead crane which grasps the vessel at trunnions on its side tocompletely drain the steel into the reducer through the oxidizer entrylaunder. This same procedure is repeated for the reducer. The finisheris bottom tapped until completely emptied into the tundish, and thetundish is bottom tapped until completely emptied into the mold.

Maintenance of melting furnace components such as the conveyor repair,electrode additions, apron cleaning, gunning or the like can beperformed in process because the melting furnace can be completelydrained without tilting. Steel can be continuously transferred to theoxidizer, processed in the refining vessels, and cast without chargingany scrap for, for example, up to 30 minutes. During this furnace delay,steel flow in the downstream vessels could be decreased to provide morebuffer time, such as up to one hour, for completing the maintenance. Ifa multiple strand caster is used, selected strands can be temporarilyplugged to provide further decrease in production rate, if necessary.

Maintenance of the oxidizer, reducer, or finisher can be performed bydecreasing flow rate in the other vessels. Steel flow in the problemvessel can be stopped while the maintenance is performed for, forexample, up to 15 minutes. For example, a slag line in one of therefining vessels can be gunned while the steel level is lowered. Each ofthe oxidizer, reducer, and finisher sits on a car that resembles a ladlecar in traditional operations. The unit can be moved to the side andreplaced with a pre-heated spare vessel if a longer delay isanticipated. Flow through upstream vessels is temporarily halted duringthe change of the problem vessel. This type of replacement can also beused to increase the duration of the continuous process by performingmaintenance on one vessel at a time.

For grade changes, alloying is halted in the reducer for alloys thatneed to be decreased during the grade change while their addition isincreased in the finisher, which dilutes the alloy concentration in thereducer while keeping the required composition of the leading grade inthe finisher. Superheating is increased in the melting furnace to offsetheat losses associated with flow interruptions. After the steeltemperature in the melting furnace, oxidizer, and reducer is increasedand the required alloy concentrations are decreased to the level of thenew grade in the reducer, flow through these three vessels istemporarily stopped, providing a break between grades. Since there is nosteel flowing into the reducer, the steel in the reducer is alloyed in abatch manner similar to ladle treatment, preparing the new grade. Thesteel in the finisher is being drained during this time, representingthe end of the leading grade. Once the finisher is drained, the furnace,oxidizer, and reducer are reopened along with flux and alloying additionrates required for the new grade during continuous operation, thusfilling the finisher with the new grade. The finisher is then reopenedafter it is filled and the steel in the tundish is lowered to minimizethe amount of intermix material similar to traditional castingoperations. Flow resumes at normal steady state after the finisher andthe tundish are completely refilled with the new grade. If the steeltemperature decreases below the necessary superheat before steady stateconditions are re-established with the new grade, the steel can beheated in the reducer, finisher, and tundish with, for example, anon-contact twin plasma torch.

It is alternatively possible to make gradual changes between grades.Currently head-to-tail grade variations in a single slab can beproblematic. These variations could be controlled by spreading out thegrade change over several slabs, gradually increasing or decreasing thealloying additions. This new procedure could decrease yield losses. Inaddition, grade changes can be controlled and scheduled to minimize theamount of downgraded intermix material.

For casters of a variety of grades, the ability to change grades in thecontinuous steelmaking method of the invention has distinct advantages.A caster which casts in, for example, 175 ton heats is currently limitedto casting each grade in 175 ton batches. Even if only 100 tons of aparticular grade are desired, the caster must make 175 tons of thegrade. And if 200 tons of a particular grade are desired, the castermust make two batches, or 350 tons. The continuous steelmaking processdoes not suffer from these limitations. Quantities of 100 tons, 200tons, and other quantities can be made, resulting in efficiency,flexibility, and cost savings over current methods.

EXAMPLE 1

Simulations were calculated for steady-state operation conditions duringfully continuous production of Si-deoxidized steel using the processmodel program Metsim (see metsim.com), and the results presented inTable 1. The Free Energy Minimizer (FEM) of Metsim was adjusted based onthermodynamical calculations, using FactSage (see factsage.com).

The simulation was based on a 165-t/hr production rate. The steel andslag masses and compositions of each vessel, as listed in Table 1, arethe result of reactions of the incoming steel stream with alloys,fluxes, and air. The extent of these reactions and the composition ofthe steel and the slag depend on the mass transfer and thermodynamicconditions within each vessel. The mass transfer rate constant (k) wascalculated by using the specific steel transport rate, which is afunction of argon flow rate, vessel geometry, steel temperature, andpressure. The thermodynamic conditions in each vessel support fastreactions and the removal of impurities. For instance, the de-S rate isincreased when less iron oxide is supplied to the bath. Iron oxidesources that include oxidized carry-over slags, oxidized sculls inladles, slag from previous heats, and iron oxides from ladle cleaningwould be minimized due to less emptying, cleaning, and refilling ofvessels and because no EAF carry-over slag will enter the reducer.

The steel temperatures were calculated during the simulation based onthe effects of additions, chemical reactions, and heat losses to theenvironment. The heat losses are based on a thermal model of therefining vessels. The current simulation results indicate that the steelonly needs to be heated in the EAF during steady-state operations. Thesteel temperature in the EAF was set to be 2908° F. based on thermalsimulations. Steel of this temperature entered the oxidizer where itcooled to 2865° F. before entering the reducer, where it cooled anadditional 29° F. The steel that flowed from the finisher into thetundish had a temperature of 2822° F. In general, the heating in the EAFis sufficient because of short processing times, efficient use of fluxesand alloys due to near-equilibrium conditions, elimination of tappinginto ladles that are below the steady-state temperatures, smallerrefractory surface area in the three refining vessels as compared tothree ladles, and additional insulation of the new refining vessels.

Based on modern Consteel operations, it is estimated that the meltingand heating of 172 tons of scrap per hour in the EAF requires 320 kWh/telectricity and the injection of oxygen at a rate of 3000 scfm. Thesteel flow from the EAF into the oxidizer is estimated to be 164 t/hr,assuming a 95% metallic yield in the EAF. The liquid EAF slag has a FeOconcentration of 14% and is in close equilibrium with the carbon contentof the steel (0.08%) due to steady-state furnace operations. The carbonconcentration of the steel in the EAF can be increased as compared tothe current EAF-LMF steelmaking route because additional de-C ispossible in the oxidizer.

The carbon and phosphorus concentrations are decreased in the oxidizerfrom 0.08% C to 0.04% C and from 0.010% P to 0.004% P due to theaddition of 4 lbs of hematite per ton of steel. The concentrations ofboth elements are increased in the reducer to 0.06% C and 0.008% Pbecause the ferroalloys contain carbon and phosphorus. The refiningconditions change from oxidizing to reducing when the steel flows fromthe oxidizer into the reducer. The stirring of the steel and theaddition of alloys and fluxes causes the de-S of the steel from 0.050% Sto 0.015% S in the reducer. Additional de-S from 0.015% S to 0.008% S isachieved in the finisher. Some aluminum reversion was calculated duringthe refining in the reducer and finisher.

TABLE 1 Example of steady-state operation conditions, flux and alloyadditions, and steel and slag chemistries for producing 165 t/hr liquidsolid steel wt % additions lbs/t slag wt % wt % total EAF (vessel 1)high Ca lime 44 electricity 320 kWh/t C 0.08 dolomitic lime 44 CaO 45 143 oxygen 3000 scfm Mn 0.20 Ca-Aluminate — SiO₂ 22 — 21 scrap 172 t/hr P0.010 bauxite — Al₂O₃ 6 — 6 capacity 55 t S 0.050 hematite — MgO 9 76 12temperature 2908 ° F. Si 0 SiMN — MnO 3 6 3 total slag 160 lbs/t Al 0FeSi — FeO_(X) 14 17 14 solid slag 4 wt % V 0 FeV — P₂O₅ 1 — 1 V3 1.61.6 Oxidizer (vessel 2) High Ca lime 3.4 capacity 27 t C 0.04 dolomiticlime 2.7 CaO 44 1 43 flow rate 164 t/hr Mn 0.17 Ca-Aluminate — SiO₂ 5 —5 temperature 2865 ° F. P 0.004 Bauxite 4.1 Al₂O₃ 22 — 22 argon 17 scfmS 0.050 hematite 4.1 MgO 9 86 10 k 0.27 min⁻¹ Si 0 SiMN — MnO 6 — 6total slag 11.6 lbs/t Al 0 FeSi — FeO_(X) 12 13 12 solid slag 2 wt % V 0FeV — P₂O₅ 2 0 2 V3 1.6 1.6 Reducer (vessel 3) high Ca lime 6.0 capacity27 t C 0.06 dolomitic lime 2.0 CaO 50 20 49 flow rate 165 t/hr Mn 0.90Ca-Aluminate 5.0 SiO₂ 18 — 17 temperature 2836 ° F. P 0.008 bauxite —Al₂O₃ 15 — 14 argon 17 scfm S 0.015 hematite — MgO 7 80 11 k 0.45 min⁻¹Si 0.26 SiMn 20.4 Mn0 nil — nil total slag 15.5 lbs/t Al 0.001 FeSi 3.2FeO_(X) nil — nil solid slag 2 wt % V 0 FeV — sulfides 10 — 9 B 2.2 2.5Finisher (vessel 4) high Ca lime 1.4 capacity 23.5 t C 0.06 dolomiticlime — CaO 48 11 47 flow rate 165 t/hr Mn 0.90 Ca-Aluminate 2.4 SiO₂ 10— 10 temperature 2822 ° F. P 0.008 bauxite — Al₂O₃ 25 — 24 argon 7 scfmS 0.008 hematite — MgO 9 89 12 k 0.17 min⁻¹ Si 0.25 SiMn — Mn0 nil — niltotal slag 4.0 lbs/t Al 0.003 FeSi — FeO_(X) nil — nil solid slag 2 wt %V 0.040 FeV 1.0 other 8 — 7 B 2.4 2.6

EXAMPLE 2

The simulation of continuous steelmaking operations was modified duringfive additional runs of the Metsim model. The final carbon, phosphorus,and sulfur concentrations after these runs are summarized in Table 2.The values of simulation 1 in Table 2 represent the results that werediscussed in the previous section and they are used as a baseline forthe other simulations.

TABLE 2 Final carbon, phosphorus, and sulfur concentrations ascalculated during six different steady-state simulations Simulation 3 45 6 Difference 2 Triple Failure of porous to 1 Double P plug in theReducer Simulation Base- production Double No de-S in ↑ Ar in 1 linerate S actions Oxdizer Finisher wt % C 0.06 0.07 0.06 0.06 0.10 0.06 wt% P 0.008 0.014 0.016 0.007 0.019 0.007 wt % S 0.008 0.019 0.018 0.0180.007 0.011

In simulation 2, the production rate (scrap and alloy addition rate) waschanged from 110 t/hr to 220 t/hr without changing the amounts of fluxadditions or the values of the mass transfer rate constants. Theconcentrations of carbon, phosphorus, and sulfur increased duringsimulation 2 as compared to simulation 1; however, they were withincommon values after ladle refining of Si-deoxidized steel. It isexpected that additional simulations will show that a proportionalincrease of flux additions and the increase of the argon stirring wouldmake it possible to decrease these concentrations to values similar tosimulation 1. The result of simulation 2 indicates that it is possibleto continuously vary the production rate during the operation of thecontinuous steelmaking process.

The effect of an initial impurity concentration increase in the scrapwithout detection was calculated during simulation 3. The phosphorus andsulfur concentrations of the steel that entered the oxidizer wereincreased from 0.010% P to 0.030% P and from 0.050% S to 0.100% Swithout changing other operational conditions of simulation 1. The finalsulfur and phosphorus concentration increased. However, they were againwithin common values after ladle refining of Si-deoxidized steel. Thisresult indicates that final steel chemistry is still within typicalsteel specifications after undetected P and S increases in the scrap.Once the impurity increase is detected, corrective actions such as anincrease in argon flow rate and flux additions can decrease the final Pand S to values similar to simulation 1.

A failure of the porous plug in the reducer was investigated duringsimulation 4. It was assumed that the swirl that is created in thevessel due to the off-center inlet stream would still result in a masstransfer rate constant of 0.05 min⁻¹ (down from 0.45 min⁻¹ during argonstirring). The simulation was calculated without changing otheroperational conditions of simulation 1. The final sulfur concentrationincreased to 0.018%, which is a common value after ladle refining ofSi-deoxidized steel. This result indicates that a failure of a porousplug does not necessarily lead to a final steel chemistry that isoutside the grade specifications.

Two corrective actions of a porous plug failure in the reducer wereinvestigated during simulations 5 and 6. In simulation 5, the operationof the oxidizer was modified by replacing the oxidizing slag with areducing slag and making SiMn and FeSi alloys additions in the oxidizer.All other operating conditions were the same as during simulation 4. Thefinal sulfur concentration of simulation 5 was lower than the finalsulfur concentration of simulation 1 because some sulfur was removedfrom the steel in all three refining vessels. The final carbon andphosphorus concentrations increased because these elements were notremoved in the oxidizer. Remarkably, the steel chemistry in the oxidizerduring simulation 5 (0.10% C, 0.019% P, 0.018% S) was similar to thefinal steel composition after ladle refining of Si-deoxidized steel.This result indicates that the steel treatment in only one of the threerefining vessels can achieve similar refining to current ladletreatment.

Simulation 6 was similar to simulation 4 with the exception that the gasflow rate and the flux additions were increased in the finisher, raisingthe mass transfer rate constant in this vessel. This change decreasedthe final sulfur concentration from 0.018% S (simulation 4) to 0.011% Swhile the final carbon and phosphorus concentrations were as low asafter simulation 1. The increase of the argon flow rate in the finisherhas the potential to increase the inclusions in the final product due toincreased turbulence and slag entrapment. Other corrective actions wouldalso be possible. For instance, the meltshop crew could have chosen toexchange the reducer on the fly after the porous plug failed.

When introducing elements of the present invention or the preferredembodiment(s) thereof, the articles “a,” “an,” “the,” and “said” areintended to mean that there are one or more of the elements. Forexample, that the foregoing description and following claims refer to“an” interconnect means that there are one or more such interconnects.The terms “comprising,” “including,” and “having” are intended to beinclusive and mean that there may be additional elements other than thelisted elements.

As various changes could be made in the above without departing from thescope of the invention, it is intended that all matter contained in theabove description and shown in the accompanying drawings shall beinterpreted as illustrative and not in a limiting sense. The scope ofinvention is defined by the appended claims and modifications to theembodiments above may be made that do not depart from the scope of theinvention.

1. An apparatus for continuous refining of steel comprising: a meltingfurnace for melting iron-bearing material, the furnace comprising a heatsource, a melting furnace inlet for continuously receiving theiron-bearing material, a melting vessel in communication with said inletfor melting the iron-bearing material and holding molten steel, and amelting furnace outlet for discharging the molten steel continuouslyfrom the melting vessel simultaneously with the melting furnace inlet'scontinuously receiving the iron-bearing material; an oxidizer having achemically oxidizing environment for oxidizing oxidizable elements inthe molten steel including decarburization and dephosphorization, andcomprising an oxidizer inlet in direct communication with the meltingfurnace outlet for continuously receiving the molten steel dischargedfrom the melting furnace outlet, an oxidizing vessel in communicationwith the oxidizer inlet for holding the molten steel, and an oxidizeroutlet for continuously discharging the molten steel from the oxidizersimultaneously with the oxidizer inlet's continuously receiving themolten steel discharged from the melting furnace outlet; and a reducerfor deoxidizing and desulfurizing the molten steel, the reducer having achemically reducing environment and comprising a reducer inlet in directcommunication with the oxidizer outlet for continuously receiving themolten steel discharged from the oxidizer outlet, a reducer vessel incommunication with the reducer inlet for holding the molten steel, and areducer outlet for continuously discharging the molten steel from thereducer simultaneously with the reducer inlet's continuously receivingthe molten steel discharged from the oxidizer outlet of the oxidizerhaving the inlet for receiving the molten steel discharged from themelting furnace outlet.
 2. The apparatus of claim 1 wherein the meltingfurnace is an electric arc furnace.
 3. The apparatus of claim 1 furthercomprising a finisher for alloying elements into and refining the moltensteel, the finisher comprising a finisher inlet for continuouslyreceiving the molten steel discharged from the reducer outlet, afinisher vessel in communication with the finisher inlet for holding themolten steel during the alloying, and a finisher outlet for continuouslydischarging the molten steel from the finisher simultaneously with thefinisher inlet's continuously receiving the molten steel from thereducer outlet.
 4. The apparatus of claim 3 wherein the melting furnaceis an electric arc furnace.
 5. The apparatus of claim 4 wherein thereducer vessel has a conical shape which tapers from a larger diameterat a top edge of the reducer vessel to a smaller diameter at a bottomedge of the reducer vessel.
 6. The apparatus of claim 5 wherein theoxidizer vessel and the finisher vessel have a cylindrical shape.
 7. Theapparatus of claim 3 further comprising: an oxidizer inlet chute at theoxidizer inlet for continuously removing slag from the oxidizer; areducer inlet chute at the reducer inlet for continuously removing slagfrom the reducer; and a finisher inlet chute at the finisher inlet forcontinuously removing slag from the finisher.
 8. A process forcontinuous refining of steel comprising: continuously feedingiron-bearing material into a melting furnace and melting theiron-bearing material therein, wherein the melting furnace comprises aheat source, a melting furnace inlet for continuously receiving theiron-bearing material, a melting vessel in communication with said inletfor melting the iron-bearing material and holding molten steel, and amelting furnace outlet; discharging the molten steel continuouslythrough the melting vessel outlet simultaneously with the meltingfurnace inlet's continuously receiving the iron-bearing material;continuously receiving the molten steel discharged through the meltingvessel outlet into an oxidizer for oxidizing oxidizable elements in themolten steel including decarburization and dephosphorization, theoxidizer having a chemically oxidizing environment and comprising anoxidizer inlet in direct communication with the melting furnace outletfor the continuously receiving the molten steel discharged through themelting furnace outlet, an oxidizing vessel in communication with theoxidizer inlet for holding the molten steel, and an oxidizer outlet;oxidizing oxidizable elements in the molten steel in the oxidizervessel; discharging the molten steel continuously through the oxidizervessel outlet simultaneously with the oxidizer inlet's continuouslyreceiving the molten steel discharged through the melting furnaceoutlet; continuously receiving the molten steel discharged from theoxidizer vessel outlet into a reducer for deoxidizing and desulfurizingthe molten steel, the reducer having a chemically reducing environmentand comprising a reducer inlet in direct communication with the oxidizeroutlet for continuously receiving the molten steel discharged throughthe oxidizer outlet, a reducing vessel in communication with the reducerinlet for holding the molten steel, and a reducer outlet; anddischarging the molten steel continuously through the reducer vesseloutlet simultaneously with the reducer inlet's continuously receivingthe molten steel discharged through the oxidizer outlet.
 9. The processof claim 8 further comprising: continuously receiving the molten steeldischarged through the reducer vessel outlet into a finisher foralloying and refining the molten steel, the finisher comprising afinisher inlet for continuously receiving the molten steel dischargedfrom the reducer outlet, a finisher vessel in communication with thefinisher inlet for holding the molten steel, and a finisher outlet; andcontinuously discharging the molten steel through the finisher outletsimultaneously with the finisher inlet's continuously receiving themolten steel through the reducer outlet.
 10. The process of claim 9wherein the melting furnace is an electric arc furnace.
 11. The processof claim 10 wherein the reducer vessel has a conical shape which tapersfrom a larger diameter at a top edge of the reducer vessel to a smallerdiameter at a bottom edge of the reducer vessel.
 12. The process ofclaim 11 wherein the oxidizer vessel and the finisher vessel each has acylindrical shape.
 13. The process of claim 10 further comprisingfeeding flux into the melting furnace, into the oxidizer, and into thereducer.
 14. The process of claim 13 further comprising feeding alloyingelements into the finisher.
 15. The process of claim 13 furthercomprising feeding alloying elements into the reducer and into thefinisher.
 16. The process of claim 13 further comprising continuouslyremoving slag from the oxidizer vessel at the oxidizer inlet.
 17. Theprocess of claim 13 further comprising continuously removing slag fromthe reducer vessel at the reducer inlet.
 18. The process of claim 13further comprising continuously removing slag from the finisher vesselat the finisher inlet.
 19. The process of claim 13 further comprisingcontinuously removing slag from the oxidizer vessel at the oxidizerinlet, continuously removing slag from the reducer vessel at the reducerinlet, and continuously removing slag from the finisher vessel at thefinisher inlet.
 20. The process of claim 9 wherein the reducer vesselhas a conical shape which tapers from a larger diameter at a top edge ofthe reducer vessel to a smaller diameter at a bottom edge of the reducervessel.
 21. A process for continuous refining of steel comprising:continuously feeding iron-bearing material having an oxygen contentbelow about 0.5% and flux into an electric arc melting furnace andmelting the iron-bearing material therein, wherein the melting furnacecomprises a heat source, a melting furnace inlet for continuouslyreceiving the iron-bearing material, a melting vessel in communicationwith said inlet for melting the iron-bearing material and holding moltensteel, and a melting furnace outlet; discharging the molten steelcontinuously through the melting vessel outlet simultaneously with themelting furnace inlet's continuously receiving the iron-bearingmaterial; continuously receiving the molten steel discharged through themelting vessel outlet into an oxidizer having a chemically oxidizingenvironment for oxidizing oxidizable elements in the molten steelincluding decarburization and dephosphorization, and comprising anoxidizer inlet in direct communication with the melting furnace outletfor the continuously receiving the molten steel discharged through themelting furnace outlet, an oxidizing vessel in communication with theoxidizer inlet for holding the molten steel, and an oxidizer outlet;oxidizing oxidizable elements in the molten steel in the oxidizervessel; discharging the molten steel continuously through the oxidizervessel outlet simultaneously with the oxidizer inlet's continuouslyreceiving the molten steel discharged through the melting furnaceoutlet; continuously receiving the molten steel discharged from theoxidizer vessel outlet into a reducer for deoxidizing and desulfurizingthe molten steel, the reducer having a chemically reducing environmentand comprising a reducer inlet in direct communication with the oxidizeroutlet for continuously receiving the molten steel discharged throughthe oxidizer outlet, a reducing vessel in communication with the reducerinlet for holding the molten steel, and a reducer outlet; dischargingthe molten steel continuously through the reducer vessel outletsimultaneously with the reducer inlet's continuously receiving themolten steel discharged through the oxidizer outlet; continuouslyreceiving the molten steel discharged through the reducer vessel outletinto a finisher for alloying the molten steel, the finisher comprising afinisher inlet in direct communication with the reducer outlet forcontinuously receiving the molten steel discharged from the reduceroutlet, a finisher vessel in communication with the finisher inlet forholding the molten steel, and a finisher outlet; continuouslydischarging the molten steel through the finisher outlet simultaneouslywith the finisher inlet's continuously receiving the molten steelthrough the reducer outlet; feeding flux into the electric arc meltingfurnace, oxidizer, reducer, and finisher and feeding alloying elementsinto the finisher; and continuously removing slag from the oxidizervessel at the oxidizer inlet, continuously removing slag from thereducer vessel at the reducer inlet, and continuously removing slag fromthe finisher vessel at the finisher inlet.
 22. The process of claim 21wherein the continuously discharging the molten steel from the finisheroutlet comprising continuously discharging said molten steel to atundish of a continuous caster.
 23. The process of claim 22 furthercomprising continuously removing slag from the oxidizer at the oxidizerinlet by the oxidizer inlet chute; continuously removing slag from thereducer at the reducer inlet by a reducer inlet chute; and continuouslyremoving slag from the finisher at the finisher inlet by a finisherinlet chute.